WO1982003156A1 - Procede et dispositif permettant la preparation d'extraits secs instantanement solubles a partir de produits naturels - Google Patents

Procede et dispositif permettant la preparation d'extraits secs instantanement solubles a partir de produits naturels Download PDF

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Publication number
WO1982003156A1
WO1982003156A1 PCT/EP1982/000049 EP8200049W WO8203156A1 WO 1982003156 A1 WO1982003156 A1 WO 1982003156A1 EP 8200049 W EP8200049 W EP 8200049W WO 8203156 A1 WO8203156 A1 WO 8203156A1
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WO
WIPO (PCT)
Prior art keywords
drying
extract
solution
extraction
adsorber
Prior art date
Application number
PCT/EP1982/000049
Other languages
German (de)
English (en)
Inventor
Ag Mittex
Original Assignee
Hussmann Peter
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Hussmann Peter filed Critical Hussmann Peter
Priority to AT82900945T priority Critical patent/ATE14505T1/de
Priority to DE8282900945T priority patent/DE3264999D1/de
Publication of WO1982003156A1 publication Critical patent/WO1982003156A1/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/26—Drying gases or vapours
    • B01D53/263—Drying gases or vapours by absorption
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23F—COFFEE; TEA; THEIR SUBSTITUTES; MANUFACTURE, PREPARATION, OR INFUSION THEREOF
    • A23F3/00—Tea; Tea substitutes; Preparations thereof
    • A23F3/16—Tea extraction; Tea extracts; Treating tea extract; Making instant tea
    • A23F3/22—Drying or concentrating tea extract
    • A23F3/28—Drying or concentrating tea extract by spraying into a gas stream
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23F—COFFEE; TEA; THEIR SUBSTITUTES; MANUFACTURE, PREPARATION, OR INFUSION THEREOF
    • A23F5/00—Coffee; Coffee substitutes; Preparations thereof
    • A23F5/08—Methods of grinding coffee
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23F—COFFEE; TEA; THEIR SUBSTITUTES; MANUFACTURE, PREPARATION, OR INFUSION THEREOF
    • A23F5/00—Coffee; Coffee substitutes; Preparations thereof
    • A23F5/24—Extraction of coffee; Coffee extracts; Making instant coffee
    • A23F5/26—Extraction of water-soluble constituents
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23F—COFFEE; TEA; THEIR SUBSTITUTES; MANUFACTURE, PREPARATION, OR INFUSION THEREOF
    • A23F5/00—Coffee; Coffee substitutes; Preparations thereof
    • A23F5/24—Extraction of coffee; Coffee extracts; Making instant coffee
    • A23F5/28—Drying or concentrating coffee extract
    • A23F5/34—Drying or concentrating coffee extract by spraying into a gas stream
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D11/00—Solvent extraction
    • B01D11/02—Solvent extraction of solids

Definitions

  • the invention relates to a method and a plant for the production of instantly soluble dry extracts from natural substances.
  • the instantly soluble dry extracts include e.g. B. the so-called instant coffee.
  • freeze drying Another type of drying is freeze drying.
  • the coffee extract is deep-frozen and then the steam is expelled as gas from the frozen coffee extract with the formation of a high vacuum and subsequent supply of heat (sublimation), so that a quickly soluble coffee granulate remains.
  • the conventional type of instant coffee production has the disadvantage that yields can only be achieved with a high use of operating and / or investment costs and a high expenditure of energy due to the high pressures and temperatures of dry matter of about 37% can be achieved, with the added fact that the aroma quality of the coffee suffers very much due to the high pressures and temperatures which are used both in the extraction and in the subsequent drying.
  • the object of the invention is to design the production of instantly soluble dry extracts from natural substances so that with a lower use of investment costs and in particular operating costs a higher yield of dry matter can be achieved relatively quickly while largely maintaining the organoleptic properties of the substances and, if the natural substance is rich in aroma and flavor, the dry substance has the highest possible proportion of these flavorings and aromas .
  • the extract solutions are prepared with different concentrations in that a quantity of the comminuted substance is first mixed with a solvent in a preliminary process, a solution being formed which is separated from the substance again and in separate amounts different concentration is divided, that the concentration of each solution is then gradually increased by each solution at the beginning of each step with a fresh
  • the particle size of the natural substance in connection with the layer height in the extractor has a decisive influence on the amount of the yield and, if it is z. B. is coffee, also on the aroma of the dry extract. It is particularly advantageous to achieve a high yield and possibly preservation of the aroma substances if the natural substance is crushed into particles with a grain size of less than 100 ⁇ , preferably 1 to 50 ⁇ , and on a filter medium in a layer height of 1 to 200 mm , but preferably 20 to 40 mm, is applied and that the extract solutions are removed again by pressure, preferably negative pressure, from the extractor.
  • the grinding in a tasteless and odorless device is carried out in two stages, essentially without increasing the temperature, with only a rough comminution in the first stage of the natural substance and in the second stage a fine grinding of the coarsely comminuted substance is to take place.
  • the amount of the yield can be increased again if the fine grinding takes place as wet grinding with the addition of extraction liquid, preferably an extract solution of the highest concentration.
  • wet grinding can also be carried out by adding a quantity of the substance leached out during the extraction, that is to say the extraction residue, to the substance to be ground.
  • a major advantage over conventional methods from the point of view of energy expenditure and, in the case of substances rich in aroma and flavor, the preservation of the aroma and the flavor, is that the extraction is carried out at least at the beginning at essentially every stage without increasing the temperature.
  • the process temperature may e.g. B. are between 15 ° C and 30 ° C. If a further increase in the yield is to be achieved without the aroma quality of the dry extract obtained being impaired too much, the extraction can be carried out at the beginning of each stage, that is to say when the solutions have a relatively high concentration, at a process temperature of 15 ° C. to 30 ° C. and towards the end of each stage, if the solutions have a relatively low concentration, at 60 ° C to 100 ° C or above. With such a temperature distribution, yields in the order of 60% can be achieved without noticeable loss of aroma and a high energy expenditure would be required.
  • the type of dehydration in the process according to the invention has the advantage that the material to be dehydrated is treated extremely gently, which is particularly important in the case of substances rich in aroma and flavor. In addition, the dehydration takes place with significantly less energy expenditure and lower general operating costs than z.
  • B. freeze drying A significant advance over conventional processes is also brought about by the fact that the condensate obtained during drying is fed back to the extraction system. On the one hand, this has the advantage that the costs for the production or
  • Preparation of the solvent e.g. distilled water can be saved, on the other hand, the flavoring substances still contained in the condensate are not lost, but ultimately benefit the end product.
  • a flavoring return can alternatively or additionally also take place in that the volatile aroma substances are added to the natural substance by means of a circulating gas flow withdrawn before the extraction process and added again after drying.
  • the extract layer is built up continuously or intermittently in a large number of individual layers, the total layer height being between 10 and 200 mm, but preferably between 10 and 100 mm.
  • the carrier for the extract layer immediately clogs when the solution to be dehydrated is applied for the first time, it is advisable to first apply a layer of extract powder to the carrier and only then to apply the solution to be dehydrated.
  • the powdered dry extract with the solution to be dehydrated can also be exposed to the gaseous drying medium. In both cases the powder agglomerates.
  • a nozzle system which has rotating nozzles has proven to be a particularly advantageous device for dispersing the solution to be dehydrated.
  • the dehydrators designed in the manner of air-supported halls are particularly inexpensive and expedient.
  • the dehumidifying device for the drying gas which has one or more rotary adsorbers as an essential component, also works in a particularly energy-saving manner. As already indicated above, the dehumidifying device is also of great importance in achieving the high aroma quality of the end product.
  • Fig. 3 shows a rotary adsorber for the drying process shown in Fig. 2, as a schematic cross section
  • FIGS. 1 and 2 show a dispersing nozzle for introducing the liquid coffee extract into the drying devices shown in FIGS. 1 and 2 as a schematic longitudinal section
  • Green coffee beans are fed to a roaster 1, in which they are thermally treated in a known manner to develop the aroma.
  • the roasted coffee beans are fed to a roaster 1, in which they are thermally treated in a known manner to develop the aroma.
  • the roasted coffee beans are fed to a roaster 1, in which they are thermally treated in a known manner to develop the aroma.
  • the roasted coffee beans are fed to a roaster 1, in which they are thermally treated in a known manner to develop the aroma.
  • the roasted coffee beans are fed to a roaster 1, in which they are thermally treated in a known manner to develop the aroma.
  • the finely ground coffee is then placed in the flatbed filter extractor 6 of an extraction system which has a battery 7 of interconnected containers 7a to 71 which are connected to the flatbed filter extractor 6.
  • the following extraction process in the extraction system takes place according to the so-called counter-current principle and serves to withdraw the extractives contained in the coffee.
  • the extraction process consists of a one-time upstream process for "setting" the concentration gradient of the container battery and a subsequent, continuously executable main process.
  • pretreated, purified fresh water preferably distilled water
  • the temperature of the solution amounts, each having the relatively low concentrations, is increased by heat exchange with a suitable medium in a heat exchanger 8, while the solution amounts of relatively high concentration essentially stay cold.
  • the container battery 7 is "adjusted" in terms of concentration, ie when the amounts of solution in the containers 7b to 71 have reached a certain concentration gradient and a certain temperature distribution, the main extraction process begins.
  • the solution concentration of the highest concentration stored in the container 7b is introduced into the flat bed filter extractor 6, into which a fresh quantity of finely ground coffee has been introduced.
  • the solution now discharged from the extractor 6 has a further increased concentration, and this amount of solution is introduced into the container 7a.
  • the solution quantity of the second highest concentration stored in the container 7c is fed into the extractor 6, where it is mixed with the coffee which has already been somewhat leached in the previous run and discharged again.
  • the solution emerging from the extractor 6 now has a concentration which previously had the amount of solution stored in the container 7b and is now also fed into the container 7b.
  • the concentrations of the solution quantities in the remaining containers 7d to 71 are increased and in each case returned to the container which in the previous pass still contained the solution with the next higher concentration.
  • the solution concentration of the highest concentration fed into the container 7a is fed via the filter or separator 9 to the drying devices or dehydrators 10 of a drying system.
  • the container 71 is filled with condensate obtained in the drying process, with residual moisture from the extractor 6, which has meanwhile been removed and replaced by fresh coffee, and, if necessary, with distilled water. The process described then begins again.
  • the liquid coffee extract taken from the container 7a in each case is dried in the dehydrators 10 by introducing it finely distributed above a filter bed into a flowing, gaseous drying medium and moving it down onto the filter bed, where it is deposited as a porous layer.
  • An air or inert gas stream which is conducted in a closed circuit is used as the drying medium and is dried again in a rotary adsorber 11 after the moisture contained in the coffee extract has been taken up in the dehydrators 10.
  • the adsorber 11 is regenerated by means of a heated, dry gas stream which, after flowing through the adsorber 11, releases its heat and the moisture absorbed in the adsorber 11 as condensate in the heat exchanger 12. The condensate is returned to the extraction system.
  • each dehydrator 10 The still coherent porous extract layer formed in each dehydrator 10 is broken down into granules by means of a rotating peeling device, which are removed from the dehydrators 10 and fed to an aroma reabsorber 13, in which the coffee is roasted, cooled, and ground in the roller mill 3 and in the aroma sorber 4, aroma substances extracted by a gas stream conducted in a closed circuit are fed again The now finished instant coffee is fed into the packaging for aroma reabsorption.
  • the coffee beans in the roller mill 3 are broken up into relatively coarse pieces in order for the subsequent fine grinding of the coffee in the ball mill 5, which is lined with porcelain, to be completely neutral in taste and smell to guarantee, to facilitate, to shorten the time or to make it possible at all.
  • the finest grinding of coffee is understood here to mean that the grain size corresponds to a sieve mesh size well below 100 ⁇ , in particular in a range from 1 to 50 ⁇ , but on average between 2 and 20 ⁇ .
  • very fine grinding means an almost colloidally fine grinding of the coffee.
  • the coffee beans pre-broken in the roller mill 3 are ground wet or dry in the ball mill 5. The wet grinding is carried out by adding a solution of the highest concentration to the pre-broken coffee beans during the fine grinding or, if such is not yet available, distilled water.
  • an aroma cycle takes place, which consists in the fact that in the last stage of roasting, during cooling, and during coarse grinding in the roller mill 3 and specifically for this purpose provided aroma sorption apparatus 4, the easily desorbable aroma substances are extracted from the coffee and the dry product in the aroma adsorber 13 is fed again.
  • the aroma sorption and subsequent integration of the aroma substances are brought about by means of an inert gas stream which flows in a circle through the individual units and devices 1, 2, 3, 4 and 13, as shown in FIG. 1 by the dashed lines, the direction of flow being the arrows is indicated.
  • the extraction system for the extraction process following the fine grinding essentially consists of the flat bed filter extractor 6 and the battery 7 of individual interconnected containers.
  • twelve such containers are provided, which are identified from 7a to 71, only the first three containers 7a to 7c and the last container 71 of the battery being shown for the sake of simplicity.
  • Each container 7a to 71 is connected at its lower end with the interposition of a shut-off valve 14 to a line 15 which, with the interposition of a feed pump 21, a shut-off valve 22 and a heat exchanger 8, to an inlet or outlet opening 16 arranged at the lower end of the flatbed filter extractor 6 leads, and via which the solution quantities stored in the containers 7b to 71 are passed to the flatbed filter extractor 6.
  • a line 23 to which the containers 7a to 71 are connected with the interposition of shut-off valves 24 with their respective upper ends and via which the solution amounts after increasing their concentration in the extractor back into the Containers 7a to 71 returned leads.
  • a feed pump 25 and two shut-off valves 26a and 26b are arranged in line 23.
  • a line 27 connects, with the interposition of a shut-off valve 29, a solvent container 28 to the container battery 7.
  • a line piece 17 branches off, which, with the interposition of a shut-off valve 18, opens into a collecting line 19 which with the interposition of a feed pump 20 and the filter or
  • Separators 9 leads to three dehydrators 10 of a drying plant.
  • a separator 31 which is connected to two vacuum pumps 32, is connected between two shut-off valves 30a and 30b arranged in line 15.
  • the flat bed filter extractor 6 consists of a closed housing 33, in which a horizontally lying grate 34 with a hexagonal or prismatic honeycomb structure is located near the bottom.
  • This grate 34 serves as a supporting base for a monofilament fabric 35, which serves as a filter or separation medium and rests on it.
  • a stirrer 37 Above the filter medium 35 is a stirrer 37 which can be driven by a motor 36 and which is designed such that it can be used not only for stirring but also for spreading cracks which form in the coffee sludge on the filter medium with increasing drying.
  • the ⁇ onofile fabric 35 is a plastic fabric based on polypropylene, polyester or polyamide with a mesh size of 10 to 40 ⁇ .
  • the extraction system works according to the so-called countercurrent principle, the container battery 7 being initially “set” in a pre-switching process and then the actual, continuously executable extraction process follows.
  • the pre-switching process for "setting" the container battery 7 proceeds as follows. Finely ground coffee is applied to the filter medium of the extractor 6.
  • the bed height of the coffee powder or, in the case of wet grinding, the height of the coffee sludge is always between 1 and 200 mm, preferably between 10 and 30 mm, even in the actual extraction process that follows later, since the extraordinary fineness of the powder or sludge Separation process at higher layers would be too difficult and mainly too slow.
  • the containers 7b to 71 are then charged with solvent from the storage container 28. Pre-treated, purified water, which may have been desalinated with an ion exchanger (not shown), but preferably distilled water, is used as the solvent.
  • the amount of solvent fed into the containers 7b is introduced via line 15 from below into the flatbed filter extractor 6, the coffee bed being whirled up and the soluble substances in the coffee dissolving.
  • the coffee powder is mixed intensively with the solvent by means of the stirrer 37.
  • the pumps 32 are switched on to suck a still thin solution through the filter or separation medium 35 out of the extractor 6 and to store it temporarily in the separator 31.
  • a filter cake is formed on the separating medium 35, which filter cake itself has a filtering and separating effect on the solid components in the coffee.
  • the cracks which form in the filter cake with increasing drying are again coated by means of the agitator 37, which has meanwhile been changed accordingly.
  • the valve 30a is closed and the valve 30b is opened.
  • the pump 25 the solution temporarily stored in the separator 31, is pumped back into the container 7b.
  • the amount of solvent fed into the container 7c is introduced into the extractor from below, mixed with the coffee which has already been somewhat leached and sucked off again as a thin solution and pumped back into the container 7b. This process is continued until the remaining containers 7d to 71 each contain a solution, the concentration of which decreases from container to container.
  • the leached filter cake in the extractor is replaced by a fresh pour of coffee.
  • the amount of solution stored in the container 7b is again passed into the extractor 6, mixed intensively with the coffee and suctioned off again as a solution with increased concentration and returned to the container 7b.
  • the procedure is carried out in a corresponding manner with the amounts of solution stored in the containers 7c to 71, so that at the end of the second pass in each container 7b to 71 there is a solution with an overall increased concentration tion. So many further passes follow until the concentration of the amount of solution in the container 7b has increased to about 40%.
  • a suitable medium such as. B. steam
  • the temperature of the amounts of solution introduced into the extractor 6 is adjusted so that the solution from the container 7b has the lowest temperature and the solution from the container 71 has the highest temperature.
  • the setting process described here is further illustrated in the table below using specific temperature values and concentrations.
  • the solution of the highest concentration is now removed from the container 7b in the case of wet grinding and mixed in the ball mill 5 with the not yet finely ground coffee powder.
  • the extractor 6 By means of the pumps 32, only the liquid contained in the sludge with the substances dissolved in it is sucked through the separation medium 35, the solid constituents remaining in the extractor 6 and, as during the setting process of the container battery 7, a self-filtering and separating filter cake form, which becomes increasingly solid with increasing withdrawal of liquid.
  • the solution emerging from the extractor 6 now has a further increased concentration. This solution is now stored in the container 7a of the battery 7 for later drying.
  • the respective concentration of the solutions in the containers 7c to 71 of the battery 7 is then increased as follows.
  • the solution from the container 7c in the Extractor 6 introduced and again so that the solid layer previously formed on the separation medium 35 is whirled up.
  • the solution is introduced from below through the opening 16 and the separation medium 35 into the area above the
  • the concentration of this solution is increased appropriately, it should correspond to the concentration of the solution which was contained in the container 7b at the beginning of the process, that is to say approximately 40% in the example, and the solution enriched in this way is also passed into the container after leaving the extractor 7b initiated.
  • the concentration of the solution amounts in the containers 7b to 71 is successively increased, the concentration of the solution of the container 7c to the value that the solution of the container 7b previously had, and the solution from the container 7c passes through the extractor 6 into the container 7b, the concentration of the container 7d is brought to the concentration that the solution of the container 7c previously had , and the solution of the container 7d passes through the extractor into the container 7c and so on, so that at the end of the battery at the end of this section of the process the solution of the container 71 is brought to the concentration which the solution of the container 7k had previously and the Solution of the container 71 has reached the container 7k via the extractor 6.
  • the solution of the highest concentration initially stored in the container 7a is then fed to the drying or dehydration.
  • the container 71 is filled again with solvent, which is composed of condensate which has been obtained during drying, residual moisture which has been obtained by squeezing out the filter cake removed from the extractor 6 and, if appropriate, a supplementary amount of distilled water.
  • Solvent has been supplied to the container 71 via the storage container 28 and the line 27. By exchanging heat in the heat exchanger 8, the amount of solvent subsequently removed from the container 71 will be increased to the temperature value which is predetermined by the "setting" of the battery.
  • the table below uses numerical values to illustrate the formation or maintenance of the concentration gradient or the temperature distribution of the solution quantities in the container battery 7 during the adjustment and main extraction process, whereby a ratio of ground coffee, which consists of a 1: 1 mixture of the Robusta coffee types and Arabica, and 1: 5 solvent was used.
  • Each dehydrator 10 consists of a housing 40, in which there is a grate or perforated plate-like carrier 41 made of a corrosion-resistant and tasteless material. Above the top of the carrier 41 is a fine-meshed fabric 42 with mesh sizes of 5 to 30 ⁇ m, preferably of monofilament, tasteless and odorless Plastics excited. This fabric is expediently the same as in the flat-bed filter extractor 6.
  • an application device 43 is arranged, which consists of a vertical tube 44 rotatably suspended from the housing ceiling and a two-armed cross tube 45 at the lower end of the vertical tube 44
  • Outlet nozzles 46 are provided on the underside of the transverse tube 45 and can be designed as rotating nozzles, single-substance nozzles, two-substance nozzles or mixing or dispersing nozzles.
  • FIG. 4 A preferred embodiment of a dispersing nozzle is shown in FIG. 4 as a schematic longitudinal section and essentially consists of a cup 47 which narrows conically upwards and is rotatably mounted about a fixed agitator 48.
  • the highly concentrated solution passes through the fixed agitator into the rotating beaker, where air or another gas is hammered into the highly concentrated solution, so that a dispersion arises that rises on the beaker wall and is thrown radially outwards through openings.
  • the highly concentrated extract solution reaches the fabric 42 via the application device 43.
  • the application device rotates continuously, so that the solution to be dehydrated is applied in layers to the fabric 42.
  • the delivery pressure, the nozzle cross-sections and the rotational speed of the application device it is ensured that, taking into account a dehumidified, gaseous drying medium which is simultaneously led through the housing and the extract layer building up on the fabric 42, the temperature at the beginning of the circulation of the application device on the fabric 42 applied extract solution until the applicator returns after a full circulation to the starting point is so dehydrated that the next layer can be taken up in such a way that the two successive layers form a bond with one another, but do not condense so that the Passage of the drying gas would be hindered, or the fine and extremely porous structure of the extract layer would be destroyed.
  • the structure of the porous layer of dried extract is very similar in structure to a porous pastry or cake.
  • a piping system 50 is provided, the valves 51 of which allow the dehumidified drying gas to be passed either from above or from below through the carrier 41, the fabric 42 and the layer which gradually builds up on the fabric.
  • the drying gas is passed through a filter 52.
  • the drying gas is conveyed using a blower 53.
  • the drying gas is dehumidified in the rotary adsorber 11.
  • a first extract layer is formed on the fabric 42 by applying the solution to be dehydrated onto the fabric 42 from above, while the drying gas is passed through the carrier and the fabric from below in countercurrent to the extract layer in countercurrent to the extract layer.
  • a fine-porous extract layer forms on the fabric 42.
  • this extract layer is formed as a separating layer between the fabric 42 and the extract layers built up thereon, the direction of flow of the drying gas is reversed, so that solution and drying gas now hit the fabric 42 from above in order to form hundreds and thousands of individual layers build up a single coherent layer that has a fine porous structure.
  • the granular but still coherent extract layer has been built up to the desired height, it is broken down into granules.
  • a rotating knife 62 which lowers in a screw or stroke shape is moved into the layer.
  • the granulate is removed from the remaining layer together with the powder resulting from this process by means of a suitable suction device.
  • a slotted tube to which the knife is attached would be conceivable as a suitable suction device.
  • the granulate and powder can also be discharged via a cyclone or a filter in the vacuum cleaner system.
  • the nozzle sen 46 are firmly attached to the housing ceiling. These nozzles could work intermittently or continuously. In the case of intermittent operation, the system switches off between the spray intervals until the sprayed-on layer has dried. In the continuous operation of the nozzles, the spray quantity must be regulated so that the sprayed-on layer dries very quickly.
  • the structure of the granules can be influenced both by the manner of application and by removal of the extract layer, so that they are e.g. B. can be approximated to that of a freeze-dried granulate.
  • the granules produced by the process according to the invention differ from conventional granules not only in their outstanding organoleptic properties, but also in their physical structure.
  • extract dust is also produced, which is partly deposited on a film 40a lining the housing. Once the granulate produced has been removed from the housing, the film is poured out using a mechanical device so that the extract dust can be collected and reused.
  • the dehydrator can be designed such that the film itself forms the housing in the manner of known air-filled halls.
  • a mechanical shaking device for shaking out the film can be dispensed with and the film can be shaken out by repeated pressure changes within the space enclosed by the film and freed from the extract dust.
  • a flexible, Teflon-coated cloth is used.
  • the adsorber 11 is a hollow cylinder and consists of individual sector-shaped chambers (FIG. 3) which are separated from one another by radial partition walls 55. They are filled with silica gel through which the drying gas is passed to be dehumidified. The drying gas thus flows in a closed circuit, which is formed by the piping system 50. The desorption of the silica gel in the adsorber 11 takes place with inert gas which is guided in a pipeline system 56. Appropriate switching devices make it possible to prepare the silica gel in one part of the chambers and to dehumidify the drying gas by means of the silica gel in another part of the chambers.
  • the adsorber consists of a total of 16 chambers.
  • the gel in the three chambers A is prepared.
  • the chambers B are connected in parallel in the primary circuit 50 so that the drying gas leaving the chambers B passes directly into the dehydrator 40 of a total of three dehydrators, in which the material to be dried is subjected to the final drying in the third drying phase.
  • the chambers B were freshly prepared with their gel immediately before the current operating phase under consideration.
  • the chambers C are located in the primary circuit 50 such that the drying gas leaving them passes to the dehydrator 40 is supplied, which works in the first drying phase, ie in countercurrent.
  • the chambers C belonged to group D of the operating phase now under consideration, which lie in the primary circuit in such a way that the drying gas leaving them is fed to the dehydrator 40, in which the material to be dried is in the second phase in the case of direct current operation the actual drying is subject.
  • the chambers of groups B, C and D are flowed through by the drying gas in parallel operation.
  • the drying gas leaving the chambers of group B enters the dehydrator 40, in which the final drying of the material to be dried is carried out.
  • this gas is diverted in order to get into chamber A1 of chamber group A in order to effect the final preparation of the gel there, ie cooling the dried gel without moistening it, the actual drying (regeneration, desorption) of the gel takes place in the chamber A2, into which the as yet unused gas of the secondary circuit 56 reaches, ie the inert gas of the highest temperature and low moisture content. Desorption takes place in chamber A2 at a temperature of approximately 160 ° C.
  • the inert gas from the circuit 56 in the chamber A2 is admixed with the inert gas leaving the chamber A1, which has the temperature which results from the cooling of the gel in the chamber A1 and which is dry.
  • the gel is preheated and pre-desorbed by the gas leaving the chamber A2.
  • the gas leaving the chamber block A is then fed to a group of heat exchangers 12, where the sensible heat still remaining, in particular the heat of condensation of the condensing gas Water to which heat exchangers are released before this gas is released outdoors.
  • the turbine 57 is also connected in the secondary circuit, the exhaust gases of which supply the inert gas of the secondary circuit 56 cleaned in an exhaust gas cleaner 58 and a filter 59 and which supplies the energy required to operate the system.
  • a fan 60 is used to convey the combustion air.
  • a sensible mixture of the gas flows in connection with the multiple use of the heat content of the drying medium results in maximum energy utilization.
  • connection of the adsorber to the piping system is changed by rotating in the direction of arrow 63 by the amount of a chamber width.
  • This can be done by appropriately switchable valves, by turning the entire adsorber or by a corresponding rotary valve.
  • the valves mean a relatively large amount of construction work, but great flexibility.
  • the Rotation of the adsorber and in particular the use of a rotary valve mean a considerable structural simplification, but a certain rigidity of the program, which is generally acceptable, however, because the same good is usually dried over a longer period of time.
  • Part of the primary air from the adsorber passes through one of the three heat exchangers, namely the one that has to be cooled in order to be ready for the next working cycle for the condensation.
  • The. Heat is absorbed by the gas of the third circuit, which z. B. heated from 20 ° C to 30 ° C.
  • the heat exchanger is then switched over as a condenser.
  • the drying process could be called a multi-stage adsorption-dehydration process.
  • the condensate obtained in the heat exchangers which may still contain flavorings, is fed back to the extraction system via the store 28 in order to be used in the extraction.
  • the dried coffee concentrate removed from the respective dehydrator 40 passes into an aroma reabsorber 13, in which the aroma substances are added to the dried coffee extract that were extracted from the coffee in the last stage of roasting, during cooling, grinding and in aroma desorber 4 and consequently have not been affected by the concentration and dehydration process.
  • the end product enriched in this way is fed into the packaging in high taste quality.
  • colloid mills instead of a ball mill, colloid mills, roller mills, pin mills or vibratory mills can also be used for the fine grinding of the coffee.
  • the grinders are tasteless and odorless and that the finely ground coffee, be it in the form of powder or a slurry, is easy to remove from the grinder or does not adhere during grinding.
  • a suitable scraper device can therefore be provided in the ball mill used.
  • the wet grinding can also be carried out by adding the leached filter cake removed from the extractor after an extraction process to the substance to be ground. This can increase the yield.
  • the filter cake which becomes particularly hard and dry in the last extraction process and sits like a wood plug in the extractor, can also be burned after it has been removed to generate heat that is to be supplied to the process.
  • the filter cake can no longer be freed from residual moisture by squeezing, since it has already dried out to a great extent as a result of the suction of the solution using a vacuum.
  • the extractor housing can also be open, because closing the housing only serves to prevent aroma substances from escaping during the extraction. It is also conceivable that the solvent or the solution is introduced into the extractor from above, but then there is no rinsing of the tissue.
  • the extraction can be varied such that the entire process section takes place at room temperature. Although the yield is somewhat reduced as a result, a particularly good aroma quality can be achieved in the final extract.
  • the heat exchanger can also be used to cool all amounts of solution, which prevents fermentation from occurring when e.g. B. the system must be shut down for a certain time.
  • a variant of the extraction also consists in that the solution amount of the highest concentration is used, among other things, to increase the concentration of the other solution amounts to the predetermined value when e.g. B. this value did not set itself due to irregularities in the system.
  • the number of containers of the extraction battery can be increased or decreased depending on the design of the system.
  • a heater could also be provided in the respective container instead of the heat exchanger or also directly in the filter bed extractor.
  • the size of the filter bed extractor can also be varied, but care should be taken must ensure that the size of the filter bed is in such a ratio to the layer height that the solution can still be sucked through the separation medium sufficiently quickly.
  • the solution should not run more quickly than 0.5 to 2 minutes.
  • the running speed can of course be increased by driving with a sufficiently high overpressure instead of underpressure.
  • the drying housing can be rigid and coated on the inside with Teflon, so that sticking of extract dust on the walls of the housing can be avoided.
  • the size of the drying housing depends on the product and is e.g. B. for non-hygroscopic substances so chosen that the yield between 300 and 800 g / m 2 / hour.
  • the extract layer built up on the carrier can also be removed by means of brushes.
  • extract powder can be sprinkled on the carrier before the first application. This powder then agglomerates with the impinging dehydrating solution.
  • the application process can also be varied so that the finished dried extract in its structure and color to that using conventional methods such.
  • B. granules produced by freeze-drying or instantizing can be approximated or made very different therefrom.
  • the dry extract which has been produced by the process according to the invention differs from conventional dry extracts by its organoleptic and physical properties.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Food Science & Technology (AREA)
  • Polymers & Plastics (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Tea And Coffee (AREA)

Abstract

Le produit naturel est finement moulu. Un procede d'extraction en continu permet d'extraire du produit naturel finement moulu les composants extractibles au moyen de solutions d'extraction de concentrations diverses par la methode du principe a contre-courant; l'extraction s'operant, du moins avec la solution d'extraction la plus concentree, sans notable difference de temperature; l'extraction s'effectuant par ailleurs de telle facon que, d'une part, l'on extrait, en vue de la deshydratation, la partie de solvant enrichie le plus fortement en extrait, - ceci apres un dernier enrichissement en extrait -, et que, d'autre part, l'on ajoute au systeme une quantite correspondante de solvant frais en vue d'une nouvelle etape extractive. La deshydratation s'opere de la facon suivante: la solution la plus concentree en extrait est finement dispersee dans un courant gazeux sec de sechage et, sous cette forme, est precipitee sur un support (41, 42), sur lequel il se forme alors une couche deshydratee d'extrait; cette couche sechee est transformee par la suite en un granule ou en une poudre d'extrait. Alternativement le courant gazeux de sechage se charge d'humidite lors de la deshydratation de l'extrait et se libere par la suite de nouveau de cette eau sur un absorbeur (11). L'absorbeur (11) lui-meme, charge d'humidite, se libere de cette humidite lors du passage d'un autre courant gazeux chaud; par refroidissement cet autre courant gazeux depose l'eau sous forme de condensat; ce condensat est reutilise en tant que solvant frais. (fig. 1).
PCT/EP1982/000049 1981-03-16 1982-03-11 Procede et dispositif permettant la preparation d'extraits secs instantanement solubles a partir de produits naturels WO1982003156A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
AT82900945T ATE14505T1 (de) 1981-03-16 1982-03-11 Verfahren und anlage zur herstellung von sofort loeslichen trockenextrakten aus natuerlichen stoffen.
DE8282900945T DE3264999D1 (en) 1981-03-16 1982-03-11 Method and device for preparing instantaneously soluble dry extracts from natural products

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3110020810316 1981-03-16
DE19813110020 DE3110020A1 (de) 1981-03-16 1981-03-16 Verfahren und anlage zur herstellung von sofort loeslichen trockenextrakten aus natuerlichen stoffen

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WO1982003156A1 true WO1982003156A1 (fr) 1982-09-30

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EP (1) EP0073807B1 (fr)
JP (1) JPS58500399A (fr)
AU (1) AU8270882A (fr)
DE (2) DE3110020A1 (fr)
IT (1) IT1228578B (fr)
WO (1) WO1982003156A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1997016073A1 (fr) * 1995-10-30 1997-05-09 Tetra Laval Holdings & Finance S.A. Procede de production continue d'extrait de cafe
CN109771976A (zh) * 2019-01-16 2019-05-21 梁振冬 一种冷热多级交替干燥塔和干燥方法
IT202100018554A1 (it) * 2021-07-14 2023-01-14 Poppi Clementino S P A Impianto ceramico perfezionato

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102006007282A1 (de) 2006-02-16 2007-08-23 Wacker Polymer Systems Gmbh & Co. Kg Verfahren zur Herstellung von kationisch stabilisierten und in Wasser redispergierbaren Polymerpulverzusammensetzungen

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1687112A (en) * 1923-03-02 1928-10-09 Magic Coffee Company Process of making liquid coffee extract
FR1001374A (fr) * 1946-04-26 1952-02-22 Gourmets Procédé et installation pour la fabrication d'extraits notamment de café ou autresapplications
US2788276A (en) * 1953-04-01 1957-04-09 Standard Brands Inc Spray drying foamed material
FR1560877A (fr) * 1967-04-22 1969-03-21
FR1566489A (fr) * 1967-03-08 1969-05-09
GB1410308A (en) * 1972-12-14 1975-10-15 Nestle Sa Treatment of condensates
GB2031570A (en) * 1978-08-11 1980-04-23 Kuri Chem Eng Method for drying water-containing substances
WO1982000596A1 (fr) * 1980-08-20 1982-03-04 Hussmann P Dispositif destine a deshumidifier un milieu gazeux de sechage utilisant un adsorbant, qui lui est regenere

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1687112A (en) * 1923-03-02 1928-10-09 Magic Coffee Company Process of making liquid coffee extract
FR1001374A (fr) * 1946-04-26 1952-02-22 Gourmets Procédé et installation pour la fabrication d'extraits notamment de café ou autresapplications
US2788276A (en) * 1953-04-01 1957-04-09 Standard Brands Inc Spray drying foamed material
FR1566489A (fr) * 1967-03-08 1969-05-09
FR1560877A (fr) * 1967-04-22 1969-03-21
GB1410308A (en) * 1972-12-14 1975-10-15 Nestle Sa Treatment of condensates
GB2031570A (en) * 1978-08-11 1980-04-23 Kuri Chem Eng Method for drying water-containing substances
WO1982000596A1 (fr) * 1980-08-20 1982-03-04 Hussmann P Dispositif destine a deshumidifier un milieu gazeux de sechage utilisant un adsorbant, qui lui est regenere

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1997016073A1 (fr) * 1995-10-30 1997-05-09 Tetra Laval Holdings & Finance S.A. Procede de production continue d'extrait de cafe
CN109771976A (zh) * 2019-01-16 2019-05-21 梁振冬 一种冷热多级交替干燥塔和干燥方法
IT202100018554A1 (it) * 2021-07-14 2023-01-14 Poppi Clementino S P A Impianto ceramico perfezionato

Also Published As

Publication number Publication date
EP0073807B1 (fr) 1985-07-31
JPS58500399A (ja) 1983-03-17
JPH0349602B2 (fr) 1991-07-30
AU8270882A (en) 1982-10-06
DE3110020A1 (de) 1982-09-30
DE3264999D1 (en) 1985-09-05
IT8209358A0 (it) 1982-03-16
IT1228578B (it) 1991-06-24
EP0073807A1 (fr) 1983-03-16

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